Note: Descriptions are shown in the official language in which they were submitted.
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METHOD AND ARRANGEMENT FOR ENERGY CONVERSION IN
STAGES
STATE OF THE ART AND PROBLEMS
An embarrassing large part during almost all energy conversions forming a
secondary/residual
heat, which pressure and/or temperature is insufficient to be interesting for
the production of
mechanical energy as electric power or other forms of useful work. The
secondary/residual
heat content of physical energy comprising beside the actual volume flow,
pressure and
temperature a large part of vaporization/condensation heat - i.e. the sensible
and latent heat
content respectively - which energy part thus is most desirable to utilize in
a more flexible
way and especially as mechanical energy, besides the electric power as an
example vehicular
motor drive as well as all means of transport. All kind of combustion are
comprising
environmental consequences by the discharge of ground near ozone 03, nitrogen
oxides NOx,
greenhouse promotion gases as carbon dioxide and unburned hydrogen carbons as
well as a
number of unhealthy particles among others as unburned carbon/char and
hydrogen carbon
particles, heavy metal particles and also aerosols. Furthermore bacteria of
legionella
constituting increasing problems into the cooling and process water systems.
The extraordinarily high enthalpy of water vaporization makes the vaporization
to a very
energy demanding process. The water vaporization during the energy conversion
by that
constitutes an extensive psychical energy uptake, when large amount of energy
is consumed.
Equivalent amount of vaporization energy is then accessible into the
steam/exhaust gas as
condensation energy. Secondary/residual heat representing the ending "energy
tail" during
most of the energy conversions - or more in common expressed; when the process
embraces
steam and/or gas turbine.
When using condensing power plants, optimized for generation of electric
power, the steam
turbine discharge of secondary/residual heat is condensed out and fed to
sewer, and this
considerable part of energy is lost. Also the steam cycle of nuclear power
plants with
corresponding condensation of the secondary/residual heat - about 2/3 of the
total energy
amount - is wasted into the recipient/see/air. During summer time it can be
restrictions about
the permissions of heat discharge into the recipients. At the combined power
and heating
plants with co-production of electric power as well as a huge part of heat,
the total energy
content of the fuel is utilized more effectively compared to the possibilities
of condensing
power plants. However, combined power and heating plants are dependent on
neighbouring
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centres of population to be saleable and fmd buyers of the too large produced
part of
secondary/residual heat. That part of energy is marketing by the energy
companies as district
heat and distributed into nets of considerable proportions. During the summer
half year, when
huge restrictions of district heat consumption, it will be marketing problems
of that energy
part resulting in forced restrictions at the synchronous electric power
generation. - thus at an
inferior economy - which has to be compensated.
Regarding carbon dioxide neutral bio-fuels into a future cycling adapted
society based on
renewable energy sources, the many different types of liquors within the
cellulose industries
have an unique position - for an example the black liquor of the sulphate
industry - and now
it is a necessity for the energy and chemical recovery of the pulp and paper
industry to be
considered from an overall perspective.
There is also a necessity for a quit new motor technology when driving all
kind of means of
transport. The conditions of climate, energy and economy are jointly forming a
complex of
problems. Thus, there is now a great necessity for a much more up-to-date and
flexible
method for an ultimate energy conversion within the whole global energy
sector!
DESCRIPTION OF THE INVENTION
Generally
The present invention offers a flexible method and arrangement for the
conversion of energy
from any kind of energy sources or fuels, by fuel synonymous substances and/or
compounds,
by energy conversion in stages when the first (I) stage of the conversion, by
a closed
circulating pressurized steam/feed water system during almost atmospheric or
pressurized fuel
combustion and/or combustion by an open partially circulated condensate system
during
pressurized thermal decomposition, stoichiometric and/or sub-stoichmetric -
the later
pressurized gasification - oxidation/combustion of at least one fuel into at
least one process
step comprising at least one pressurized reaction/combustion chamber, when
said
oxidation/combustion/gasification into the open system occurring during
increased steam
partial pressure by the fuel content of hydrogen and/or water and/or water
supply into the fuel
and/or into the connection to the said thermal decomposition, said water
supply preferably by
hot recovered/circulated condensate, when both the systems first (I)
conversion stage is
followed by a prolonged conversion via the second (II) stage, which second
(II) stage
constituting condensation cooling in steps through at least one expander
turbine or similar
apparatus of type rotating machine comprising at least two partial steps with
preferably
intermediate separation of feed water/condensate, by the first (1) conversion
stage
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produced/utilized energy comprising by the vaporization of the feed
water/condensate
generated pressurized mass flow containing sensible and latent heat, whereupon
condensation
cooling occurs during mainly counter current fed media of lower temperature
against media
before of higher temperature, comprising feed water/condensate fractions for
direct or indirect
heat traõsmission or another medium for indirect heat transmission comprising
fuel, oxidizing
agent and/or cooling medium cycle, during preheating/vaporization of the
cooling medium -
when needed during superheating - while hot condensate constitutes said water
supply into
the reaction/combustion chamber within the open system, while the feed water
is circulated
within the closed system steam cycle, and while the condensation cooling
preferably is ended
during vacuum and at the open system with separation of clean and cold
condensate excess,
while said cooling medium cycle constitutes the third (III) conversion stage
at the same time
as the first (I) and second (II) conversion stages, with or without co-
operation through the
third (III) conversion stage, producing mechanical energy as electric power
via turbine
connected generators or to be utilized for a stationary machine/apparatus or
any kind of
vehicular/means of transport at land, see or into the air.
An open partial circulating condensate system has earlier been described
through the Swedish
patent C2 526 905.
The method of the energy conversion in stages within both the closed as well
as the open
system comprising an extensive both system and stage integration, which makes
possible an
effective conversion of heat/chemical energy to mechanical energy during most
of the entire
temperature drop.
The pressurized combustion/gasification of the open system - some kind of a
turbo system -
during increased steam partial pressure preferably takes place within the
pressure interval of
2-220 bar (a) and the temperature interval of 300-3100 C with generated mass
flow
preferably within the temperature interval 100- 1400 C and the fractionated
condensate
recovery mainly within the temperature interval 10- 370 C. The higher
condensate
temperature area involves the corresponding very high liquid heat of the
condensate, which is
recovered by the return into the combustion/vaporization chamber. The lower
temperature
area - preferably created during vacuum - means cooled both the flue gas as
well as the
condensate excess.
The extraordinarily high enthalpy of water vaporization makes the vaporization
into thp
reaction/combustion chamber to a very energy demanding process - a huge
physical energy
uptake - with the corresponding contribution of physical energy to the gas
phase/mass flow.
This vaporization work is later on recovered as mechanical energy via the
condensation
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energy by the expander turbines and the counter currant step-by-step fed
condensate fractions.
The water/condensate constitutes by that an intimate natural and effective
energy carrier
between the sequences vaporization/energy up take and the condensation/energy
delivery. The
effect of the condensation is secured by the third (III) conversion stage
and/or by the heat
exchangers of the expansion cooling by utilizing a part of the heat content of
the feed
water/condensate and/or the steam-/gas-/condensate flows to preheat/vaporize
suitable media
of lower temperature - for example cooled compressed/liquid fuels/oxidizing
agents in the
form of natural gas hydrate NGH and/or Liquid Natural Gas LNG, hydrogen as
well as
oxygen etc. The utilization of liquid natural gas LNG as a fuel is achieved by
cooling the
natural gas down to about minus 160 C, whereby the volume of the fuel is
decreased to only
about 5-10 % of the original volume and by that simplified for transport.
However, there is a
necessity for a large amount of heat to vaporize LNG at the combustion site,
which heat thus
is recovered by the condensation cooling. In the same way other liquids/com-
pressed media
are vaporized as for example liquid hydrogen of temperature minus 253 C.
By the invention all kind of conventional ineffective condensing power plants
are eliminated,
including the feed water/steam cycle of nuclear power plants which will be
much more
eff-icient, as well as the demand of the combined power and heating plants for
neighbouring
centre of population with corresponding extensive district heating net is
eliminated/limited,
whereby now there is a possibility to locate plants for energy conversion
close to available
fuels - as depot or feed pipe for natural gas and hydrogen, domestic waste and
forest local
bio-fuels, which fuels do not need to be transported far away within extensive
collecting
areas. Regarding nuclear power plants the necessity of location close to
seaside or enormous
cooling towers are eliminated. The increasing problem caused by bacteria of
legionella into
the cooling and process water system is eliminated by the unnecessarily
cooling towers.
The first (I) stage of the energy conversion also comprising reaction heat
from any kind of
process heat and/or another heat, comprising the recovery of calcination
energy and
geothermal heat, also comprising conventional energy conversion as well as
pressurized fuel
cell or more in common expressed: where steam and/or gas turbine are involved,
which
secondary/residual heat to day representing unavoidable and huge "energy
tail".
The first (I) and second (II) stages of the energy conversion, furthermore
within the open
system, comprising a mostly essential cleaning method of the inert gases
originating from the
first (I) conversion stage of the pressurized combustion and/or gasification,
after which by the
second (II) stage condensation out of unburned and unhealthy gas carried
particles and
aerosols from ultra fine sizes about 0,01 and larger as well as strongly
greenhouse
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promotion gases of unburned hydrogen carbons, which are returned by the
preheated counter
current fed condensate for destruction by injection into the fuel and/or in
connection to the
reaction/combustionlvaporization chamber of the first (1) conversion stage.
The increased
water steam partial pressure H20 of the combustion stage is reducing the
partial pressure of
the hydrogen carbon compounds as CH4, whereby the ending oxidation of char and
the
remaining hydrogen carbons are improved - some kind of steam reforming:CH4 +
2H20
CO2 + 41-12 - at the same time uncontrolled local zones of high temperature
are eliminated,
which counteracting the generation of for the environrnent and health care
harmful agents and
compounds as ground near ozone 03 and nitrogen oxides NOx.
The present invention thus eliminates/restricts hot water production of the
conventional
energy conversion and by that also the restricted fixed production relation of
hot water vs.
electric power, whereby offers by the energy conversion in stages a flexible
method and
arrangement of producing mechanical energy as electric power by the heat of
combustion
during almost the entire temperature drop. Thanks to that the production of
secondary/residual
heat in the state of forced district heat is eliminated/restricted, which heat
potential for
example in stead is maintained by a system of conventional electrically driven
local
arrangement of heat pumps during extremely high total energy efficiency, or
the power used
in another way. The energy conversion in stages thus involves also this
arrangement of local
heat pumps, constituting the very best economic and environmental friendly way
for
according to the needs real long distance efficient heat supply, which in this
case representing
the ending fourth (IV) stage of the energy conversion - an economically and
environmentally
great technology leap - which in addition also makes possible an integrated
energy efficient
co-production of both heat as well as cold by cooling plants during a very
high total energy
factor.
Concerning fuels and by fuel synonymous substances and/or compounds includes
part or parts
of hydrogen, hydrogen compounds and hydrogen carbon compounds - including all
kind of
fossils, but most of all renewable/carbon dioxide neutral bio-mass as forest
residuals, peat,
rapidly growing aspen, poplar, salix and straw fuels, vegetable and animal
oils and grease,
digested/bio-sludge, bio-gas etc. and fuel gas from gasification as for
example liquors of the
cellulose industries, when pre treatment/evaporation of these liquors is best
done integrated
with the gasification. The application of the invention within the energy and
chemical
recovery of the cellulose industries stands in a sharp contrary to the
standpoint of the
technology, representing according to the needs a great technological leap.
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Furthermore one valuable energy source within the cellulose industry is
represented by the
endothermic calcination energy, which corresponding fuel supply is about 40
litres oil per ton
of pulp, and this fuel supply is recovered as electric power by the invention.
An exceptional position among fuels/energy carriers constituting steam
generating substances
and/or compounds, comprising hydrogen H2 and hydrogen peroxide H202, which
energy
conversion are well adopted by the method, among others by the exothermic
decomposing
reaction of hydrogen peroxide by the large thermo dynamical energy content as
well as the
stabilising influence on the combustion/gasification process by hydroxide
radicals.
Concerning burner nozzles of the reaction chamber all kind of single-/multi-
hole nozzles are
included - with or without infra/sonic sound generating effect. When use of
solid/half solid
fuels of type powder, chips and domestic waste etc., the method embracing
tightened plug
screw feeders PSF.
When oxygen is used as an oxidizing agent followed by the effective
condensation of the
treated flue gas, the gas contains in principle only carbon dioxide, which
simplifies the
handling of carbon dioxide as by partial return into the reaction/combustion
chamber and/or
for sale or long time storing deep into see, or into different geological
formations according to
the international proclamation "Carbon Dioxide Capture and Storage" - CCS.
The present invention thus involves a binary system by the energy conversion
in stages,
comprising both the first (I) and second (II) stages of the high temperature
loop and when
appropriate followed by the third (III) stage of a low temperature loop,
whereby opportunities
are created for a flexible and up-to-date conversion of heat/mass flow into
mechanical energy
almost during the entire temperature drop.
When appropriate a chemical recovery in the state of solid phases of dissolved
slag/melt
and/or as gas phases are integrated. There is a possibility for an extensive
heat exchange
integration between the high and low temperature loops, whereby the energy
conversion is
effected during a minimum of exergy losses during considerable improved
efficiency for the
production of for example bio-fuels as well as mechanical energy, which
comprising the
global entire energy sector during long-term sustainable economy and
environment.
The most essential process criteria of the invention comprising, from an
expansion point of
view, an energy rich gas and/or steam phase 24 which besides the pressure and
density
consisting of an ultimate volume/mass flow including sensible and latent heat,
which within
the open system includes optimization of the operation criteria as flow and
temperature of the
circulating hot contaminated condensate 20, by the liquid heat specific
enthalpy hf kJ/kg,
which is returned into the reaction chamber etc. for an effective direct
acting vaporization.
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Figure 1
The figure describes in general the second (II) stage of the counter current
expansion cooling
during a closed system for feed water handling within some kind of steam/feed
water cycle.
The arrangement comprises feed water preheating by the counter current fed
condensate/feed
water fractions, simultaneously the condensation effect of the expansion
cooling is more
effective above all by the possibility into the counter current fed condensate
fractions - as an
alternative into the discharge of the expander turbines, which is more evident
by later figures
- install heat exchangers for in-direct cooling by one or more media. The
number of described
expander turbines can be both more or less - and as an alternative with
individual shafts and
generators.
The primarylsecondary/residual heat/mass flow 24 connects expansion turbine 6
after which
the discharge pipe 25 connects device 10 for a first separation of
condensate/feed water 20
from steam flow/residual heat 26, which connects expander turbine 7 after
which the
discharge pipe 27 connects device 11 for a second separation of
condensate/feed water 19
from steam flow/residual heat 28, which connects expander turbine 8 after
which the
discharge pipe 29 connects device 12 for a third separation of condensate/feed
water 18 from
steam flow/residual heat 30, which connects expander turbine 9 after which
follows an ending
separation of condensate/feed water 17 by when appropriate vacuum strengthened
barometric
fall leg 14 with water seal/tank 15. Supply of feed water 170 occurs for
example at the rear
part at start up and during operation when needed by feed water of lower
temperature, when
condensation cooling constitutes an integrated part of an entire whole feed
water system, after
which corresponding amount of feed water of higher temperature is separated by
some of the
front fractions for example 18 or 19 as the pipe 19A. Fractions of
condensate/feed water are
fed counter currant and stepwise by pipe 17 to the discharge 29 via
arrangement 171, by pipe
18 to the discharge 27 via arrangement 181, by pipe 19 to the discharge 25 via
arrangement
191, after which preheated condensate/feed water 20 returns into actual energy
source or
utilized in another way, which is cleared by later figures. There is thus a
possibility to utilize
the heat content of the condensate/feed water for preheating and/or
vaporization of suitable
media resulting in a more effective condensation cooling, for exa.mple by heat
exchangers
115, 116 and 117 connected in series or in parallel in condensate piping 17,
18 and 19
comprising the cooling medium of a cooling cycle, oxidizing agent and/or fuel
and/or external
coolant.
The expander turbine generator 38A generates electric power 45 - as follows to
be shortened
named as power 45.
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Figure 2
The figure describes in general the second (II) stage of the expansion cooling
during an open
system for condensate handling. The arrangement comprises condensate
preheating by the
counter current fed condensate; simultaneously the condensation effect of the
expansion
progress is more effective - by the possibility within counter current fed
condensate fractions,
as an alternative/complement into the discharge of the expander turbines,
install heat
exchangers for in-direct cooling by one or more media.
The pressurized flue gas/steam mixture constitutes a
primary/secondary/residual heat/mass
flow 24 and connects expansion turbine 6 after which the discharge 25 connects
a device 10
for a first separation of condensate 20 from gas/steam mixture 26, which
connects expander
turbine 7 after which the discharge 27 connects device 11 for a second
separation of
condensate 19 from gas/steam mixture 28, which connects expander turbine 8
after which the
discharge 29 connects device 12 for a third separation of condensate 18 from
gas/steam
mixture 30, which connects expander turbine 9 and after which the discharge 31
preferably
during vacuum connects device 13 for a last separation of cold, clean
condensate excess 16
and treated cold flue gas 33 via fan 32. The discharge pipe 31 can when
appropriate have a
complementary condenser step - heat exchanger 114 with an external coolant -
according to
dashed lines. Counter current fed condensate fractions, as well as the ending
vacuum
generating barometric fall leg 14 with water seal/tank 15, achieve together a
prolonged
condensation cooling/energy recovery. Addition of external water 170 occurs -
for example at
start up and when needed during operation, when preheated condensate/water is
separated at
the front steps for example by pipe 18A. Condensate transports counter current
and stepwise
according to previous Figure 1, after which preheated condensate 20 returns
into actual
energy source or utilized in another way. The generator 38A of the expander
turbines is
producing power 45.
There is a possibility to separate/recover non process elements NPE/heavy
metals 20AA from
circulating condensate 20 and/or from other condensate fractions.
There is a possibility to utilize the heat content of the condensate fractions
by heat exchangers
115, 116 and 117 according to Figure 1.
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Figure 3
The figure exemplifies the energy conversion during stages, of a closed
condensate/feed water
system corresponding to Figure 1, in the state of a boiler complete with
steam/feed water
cycle for a conventional combined power and heating plant representing the
first (I) stage of
the conversion, but thanks to the invention constituting a power plant for
power generation.
The discharge/counter pressure of secondary/residual heat/mass flow from a
conventional
energy conversion by high and low pressure steps of steam turbines is
condensation cooled by
the additional second (II) stage of the conversion by an arrangement of three
steps of
expander turbines and a counter current return of preheated feed water to the
steam boiler.
The heat content of respective feed water fractions can earlier have been
utilized for the
preheating/vaporization of combustion air and/or fuel - when the total energy
efficiency and
the entire condensation effect are improved.
Fue135 and combustion air 34 supplies the boiler 2 for the production of steam
23A into at
least one high pressure turbine 5A which discharge 23B, eventually after moist
separation and
inter stage super heating, is fed by pipe 23C into at least one low pressure
turbine 5B
preferably with for the steam turbines jointly shaft driven generator 37 for
the production of
power 45 with a steam discharge 24 from the low pressure turbine 5B, which
discharge/counter pressure 24 of secondary/residual heat/mass flow - the
energy tail of a
conventional energy conversion, is expansion cooled by the invention by three
steps in series
of expander turbines 6, 7, and 8 with generator 38A for the production of
power 45. There is a
possibility to feed a part flow 23BB from the discharge of high pressure
turbine 5A to the
inlet of low pressure turbine 5B according to dashed lines. The pipe 24
connects device 10 for
a separation of feed water 20 from the residual heat 24A, which connects
expander turbine 6
after which the discharge 25 connects device 11 for the separation of feed
water 19 from the
residual heat 26, which connects expander turbine 7, after which discharge 27
connects device
12 for further separation of feed water 18 from residual heat 28, which
connects expander
turbine 8 which discharge of feed water 17 is fed counter current and step
wise into the
discharge 27 via arrangement 171, by the pipe 18 into the discharge 25 via
arrangement 181,
by the pipe 19 to the secondary/residual heat/mass flow 24 via arrangement
191, after which
preheated feed water 20 returns into boiler 2 when suitable via heat exchanger
21 for still
more preheating by hot flue gas 33 and into the boiler renewed production of
steam 23A,
when the loop is completed. Feed water refill 170 and the installation of heat
exchangers 115,
116 and 117 according to previous Figure 1.
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Figure 4
A high temperature loop 100 and a low temperature/cooling medium loop 200 of a
binary
system are exemplified by the presented TS-diagram, which cooling medium loop
200 is
expressed in the form of an "Ideal Rankine Cycle with Superheat". The
exemplification is
only in general form when both the loops are shown within the same medium.
The upper loop 100 starts at pos. I, by pressuring the condensate/feed water
by pump P 1 up to
pos. II, after which the combustion of the fuel takes place during constant
pressure and moves
the medium/mass flow to pos. III, after which the medium is expanded into at
least one gas
and/or steam turbine and/or expander turbine to pos. IV with completed
condensation by one
or more heat exchangers - among others in mutual with cooling medium loop 200 -
of the
secondary/residual heat back to start position I and the pump P 1, and the
upper loop is
completed.
The lower loop 200 starts at pos. 1, by pressuring the cooling medium by pump
P2 up to pos.
2, after which preheating/vaporization occurs by above mentioned heat
exchangers, in mutual
with the loop 100, during constant pressure to pos. 3 with the following super
heating by
appropriate heat exchanger up to pos. 4, after which follows expansion by at
least one turbine
204 or similar apparatus of corresponding function of type rotating machine
down to pos. 5
with an ending condensation of the cooling medium by one or more heat
exchangers during
constant pressure to pump P2 and the start position 1, representing the lower
isotherm of the
diagram, after which the lower loop is completed. The actual heat exchangers
are exemplified
as rectangles and when necessary includes external coolant. There is a
possibility not to
superheat the vaporized cooling medium 200, when the expansion takes place
between pos. 3
and pos. 6 according to dashed line, when partial condensation occurs already
during the
expansion. The stressed line between pos. 2-3-4 is only generalized and
represents the
vaporization/superheating of the cooling medium and comprises the integrated
cooling part of
the energy conversion of both the first (I) and second (II) stages during
counter current fed
condensate fractions by actual heat exchangers within the high temperature
loop 100. The
cooling medium 200 comprises for the process/temperature area suitable process
criteria as
volume flow type of cooling medium - for example - ammonia NH3, HFC, R290 or
anything
else.
The far driven integration of the binary system stages I, II and III makes the
energy
conversion possible of produced and/or extem heat supply/mass flow into
mechanical energy
during high total energy efficiency, comprising production of power 45 and/or
operation of
stationary machine/apparatus or mobile machine/means of
transpordvehicular/craft 41.
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Figure 5
The figure exemplifies the first (I) and second (II) stages of the energy
conversion of a closed
condensate/feed water system with the integration of a third (III) stage,
which stage consists
of a cooling medium cycle 200 - the low temperature loop within the binary
system. As the
conventional boiler energy conversion with adherent steam turbines represents
the first. (I)
stage of the energy conversion, while the residual heat condensation cooling
by the expander
turbines constitutes the second (II) conversion stage, which both stages make
up the high
temperature loop 100 earlier has been described, by that the exemplification
only covers the
cooling medium cycle 200.
The cooling medium cycle comprising for the process/temperature area designed
pressure and
amount and type of cooling medium - for example ammonia NH3 - when the loop
starts by
pump P2, after which pressurized liquid cooling medium through pipe 202, by in
turns and
counter currant, passes the heat exchangers/vaporizers 115, 116, 117 and 118
into respective
condensation fractions after which the cooling medium - now preferably in gas
phase,
eventually superheated - is fed through pipe 203 into at least one expansion
turbine 204, or
similar device, with generator 38B for the production of power 45,
alternatively also turbine
driven pump P2, and with the cooling medium now as one-phase or two-phase
liquid/gas
mixture. The cooling medium is fed by piping 205 into heat exchanger/condenser
112A,
which represents pre heater/vaporizer for the fuel 35-35A, in order to lower
the cooling
medium temperature together with the following condensers I 12B, after which
condensate
fraction 19 is distributed as 19 and/or 19A, and by pipe 206 the cooling
medium passing the
condensers I 12C and 112D for preheating condensate fractions 18 and 17
respectively, after
which the cooling medium now again is in liquid form and by pipe 207 fed into
pump P2, and
the loop is completed. When necessary, one more condenser 112E is installed
with an external
cooling medium before pump P2.
Figure 6
This figure represents a modification of the earlier description of the closed
system by
reducing the number of turbine steps to two - pos. 6 and 7- and changed
positions of the heat
exchangers/vaporizers/super heater 116 and 117 into the discharge pipe of the
expanders for
an alternative/strengthened condensation cooling. There is a possibility to
circulate part of the
condensate fraction 20 by the flow 20A (according to dashed line) in order to
control the heat
transmission at heat exchanger/vaporizer 117. The cooling medium cooled feed
water fraction
19 is re-heated by condenser 112B before the return to boiler 2 by the entire
condensate 20.
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The exemplified expander turbine step 5 can be used as both high and low
pressure turbines in
accordance with Figure 3.
When appropriate additional condensing capacity is installed by heat exchanger
112C.
Figure 7
The arrangement exemplifies the energy conversion in stages, the first (I) and
second (II)
stages of the high temperature loop 100, by an open system according to the
general Figure 2
as a hole, embracing the first (I) energy conversion reaction chamber 1 for
pressurized
combustion/vaporization - some kind of a turbo method - by the supply of fuel
35/11 IB,
oxidizing agent 34 and preheated condensate 20 by injection into fuel and/or
in connection to
the reaction chamber 1. The temperature as well as the steam partial pressure
of the
exhaust/flue gas 33 is settled by the returned hot condensate fraction 20 of
the counter currant
condensation cooling as well as the counter/discharge pressure 31 of the
expander 9,
preferably during vacuum in accordance to earlier descriptions.
When for example use of liquid natural gas as a fuel 35/111B the vaporization
heat takes
from the condensation heat exchanger 112A according to previous descriptions.
When necessary the condensation effect at pipe 31 before the exhaust can be
strengthened by
an additional condenser 114 as an external coolant according to dashed
marketing.
Figure 8
The above described figure within the open system is modified by reducing the
number of
expander turbine steps to three - 4/6, 7 and 8- and the air compressor 3 is
shown as well as a
require controlled/restricted municipal heating network 20F and the
integration of a cooling
medium 200 in accordance with earlier descriptions. As an alternative the
expander turbine 6
can be replaced by a gas turbine as shown by pos. 4. When necessary additional
condenser
capacity is installed by heat exchanger 112C.
Figure 9
The figure describes both the first (I) and second (II) stages of the
conversion within an open
system, with the integration of a cooling medium cycle 200 of the third (III)
stage according
to previous descriptions, besides the changed position of heat exchangers 115,
116 and 117 of
the figure which are installed into the discharge piping of the expander
turbines.
There is also a possibility to install the heat exchangers, as for example 117
in the pipe 25, for
a condensate recovery in counter current position vs. the gas flow, resulting
in an effective
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13
heat exchanger wash, which is not cleared by figure. When necessary additional
condenser
capacity can be installed in pipe 207, which is not cleared by figure.
Figure 10
This figure describes a modified method of the previous figure, by replacing
the cooling
medium of the low temperature loop 200 by the preheating/vaporization of fuel
1 I 1 A-111 B -
preferably as liquid hydrogen and/or liquid natural gas, natural gas hydrate
or equal.
There is a possibility - by some modifications - the figure also representing
a quit new
rotation motor technology for vehicular drive according to later Figure 14.
From an environmental point of view interesting possibility when using fuels
producing
carbon dioxide preferably in combination with oxygen 120 as an oxidizing
agent, is to
compress the condensation cold/cleaned flue gas of close to only carbon
dioxide 33A to be
forced down deep into see or appropriate geological formation for long-time
storing - in
accordance with dashed marking - which by the way is possible at most of the
exemplifications within the open system. Also oxygen 120 is to be preheated
and vaporized
by available condensation heat, which is not cleared by figure, when the
compressor 3 in stead
is utilized for the compression of carbon dioxide 33A.
Figure 1 i
The figure describes energy conversion within a closed stearn/feed water
system in
accordance with earlier descriptions, but here the steam is produced at any
kind of nuclear
power plant 43 with subsequent generator equipped steam turbines -
representing the high
temperature loop 100 of the binary system. By more or less replacing the
conventional
condensation cooling of the steam turbine residual heat including dumping into
recipient, all
or most part is instead by the invention - below the horizontal marked line -
converted into
preheated feed water and power 45. Thanks to the invention the need for coast
near
installation or enormous cooling towers is eliminated.
Steam 23A within the first (I) stage of energy conversion, at for example 60
bar (a) and 280 C
connects at least one high pressure steam turbine 5A which discharge 23B -
eventually after
moisture separation and an intermediate stage of super heating - connects at
least one low
pressure steam turbine 5B by the pipe 23C at for example 10 bar (a),
preferably by for the
turbines in a jointly shaft driven generator 37 for generation of power 45
with the residual
heat discharge 24 from the low pressure steam turbine 5B for example within
the area of 0,7-5
bar (a), which residual heat 24 connects the second (II) stage of the energy
conversion by
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expander turbine 6, after which from the expander turbine 6 discharge of
residual heat/feed
water 25 passes heat exchanger/super heater 117 within at least one cooling
medium cycle
200 and after that device 10 for separation of feed water 19 from residual
heat 26, which
connects next expander turbine 7, during power generation via generator 38A,
after which the
discharge of residual heat/feed water 27 passes heat exchanger 116 within a
cooling medium
cycle, for the fina.l condensation of the residual heat 27 preferably during
vacuum, after which
feed water 17 connects the heat exchanger/condenser 1 i2B of the cooling
medium cycle for
simultaneous preheating, after which feed water as fraction 18 connects the
pipe 20 and/or by
pipe 18A (dashed line) the discharge 25 of expander turbirie 6 after which the
separated feed
water 19 by device 10 connects the heat exchanger 112A of the cooling medium
cycle for
simultaneous preheating the feed water as fraction 20, which representing the
nuclear power
plant 43 feed water cycle, after which the steam flow 23A is ready for another
steam/feed
water cycle.
When requiring more condenser capacity this is to be installed in the cooling
medium cycle
by heat exchanger I 12C with an external coolant and/or in another suitable
medium to
support the condensation.
The cooling medium loop 200 is chosen according to the needs and the loop has
been
described by previous figures.
Power 45 is thus produced via the first (I) stage generator 37, the second
(II) stage generator
38A as well as the third (III) stage generator 38B.
Figure 12
The figure exemplifies the energy conversion in stages by a pressurized fuel
cell representing
the first (1) stage of the energy conversion. This fuel cell is producing, in
accordance with
otherwise known process, both power as well as steam but with the difference
by the
condensation cooling system the recovered hot condensate returns to the fuel
cell to be
vaporized and for a temperature control of the produced mass flow. The higher
temperature of
the pressurized fuel cell - in relation to an atmospheric one - gives a higher
efficiency and
facilitates the conversion of hydrogen and oxygen to steam and power during
less/without
costly catalyst - for example platinum. Both the fuel and oxidizing agent
represents a number
of hydrogen and oxygen containing substances and compounds comprising besides
hydrogen,
oxygen and hydrogen peroxide, also dimethylether DME, alcohols and
conventional hydrogen
carbon compounds. Liquid hydrogen, oxygen and natural gas LNG can be vaporized
by heat
exchanger 115, 116 and 117 according to earlier descriptions.
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Pressurized fuel cell 44 is supplied fuel/energy carrier 35, oxidizing agent
as compressed air
34 and/or oxygen 120 and circulated preheated condensate 20, when power 45 and
steam/gas/mass flow 23 is produced, which connects the expander turbines
directly for
condensation cooling according to dashed marking 23/24, or connects any kind
of at least one
step of steam turbine/rotating turbo machine 5 as an intermediate step, after
which the
discharge 24 or 23/24 connects by Figure 2 generally described condensation
cooling by the
four steps of turbine 6, 7, 8 and 9 including counter current fed condensate.
The arrangement
producing power 45 by both fuel cell 44 as well as via generators 38A and when
appropriate
37. When utilizing fuel without carbon content, no carbon dioxide containing
flue gas is
produced and the fan 32 and chimney 33 are excluded, which is not cleared by
figure.
The counter current fed cooling medium cycle 200, in accordance with previous
figures, can
be utilized also within this arrangement, which is not cleared by figure.
Figure 13
This figure describes the very great flexibility and the great number of
varieties of the present
invention in the form of recovering energy and chemicals from liquids within
the cellulose
industry - for example black liquor. The high temperature loop of the binary
system
comprising a pressurized reducing process step followed by a pressurized
oxidizing step, both
steps are integrated by a low temperature cooling medium loop 200, which
medium is fed
counter current, both internally within respective process step as against
both the process
steps order, where by the stepwise vaporization of the cooling medium loop
starts within the
ending process step, after which the vaporization of the medium is completed
within the first
process step before - preferably during superheating. After that the cooling
medium loop
passes by in turns at least one expander turbine - or similar device - with
generator, preferably
without any condensation, and after that four heat exchangers/condensers with
the possibility
for if necessary additional condenser capacity by some external cooling medium
(not cleared
by figure), after which the cooling medium is liquefied and the loop is
completed.
The reducing process step includes a fuel gas cleaning step during preferably
partial moisture
condensation, followed by the oxidizing process step of almost complete
moisture
condensation of the flue gas. The first process step comprises reaction
chamber for the
gasification/vaporization with the adherent quench as a dissolver of the
recovered
melt/chemicals - mainly Na-/K-compounds. There is also a possibility for a
recovery of
chemicals from the reducing fuel gas phase as synthesis gas (H2 and CO), which
can be
obtained for the production of for example hydrogen peroxide (H202) and/or a
number of
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different mobile automotive/bio fuels comprising hydrogen, dimethylether (DME)
and
methanol (CH3OH).
The reducing process step of fuel consists of black liquor preferably of lower
dry substance
content with kept natural amount of sulphate soap - and the oxidizing process
step of fuel
consists of by the previous step produced fuel gas and as a possibility with
an additional fuel
supply. This supply for example comprises bio gas or some kind of natural gas -
which
preheat'ing/vaporization, also includes liquid oxygen, representing a part of
mentioned heat
exchanger/condenser of the cooling medium loop.
The entire black liquor recovery process can be both simplified and more
effective by
excluding the conventional separation step of the energy rich sulphate soap
within the
evaporation plant, resulting in an increased obtainable synthesis gas and/or
power
corresponding to the high energy content of the into the black liquor left
sulphate soap.
The operation criteria of the reducing first process step are preferably high
operation pressure
as well as high steam partial pressure, and with respect to the carbon
conversion lowest
possible operation temperature into the gasification reactor, which makes
possible an effective
split of alkaline and sulphur compounds - the later as hydrogen sulphide (H2S)
as a part of the
fuel gas. The recovery of hydrogen sulphide, which only is cleared by the
figure in principle,
occurs by conversion to elementary sulphur S and/or by selective absorption in
alkali
preferably by some kind of short time contactor - one or more static and/or
dynamic devices
preferably in counter currant series - and/or the production of polysulphide
and/or the supply
of S and/or 1-12S into another reaction chamber for gasification of a partial
flow of black liquor
- and/or another liquor, for example when appropriate sulphate soap - at low
operation
pressure, approx. 2 bar(a), for in the reaction chamber direct
conversion/production of high
sulphidity white liquor NazS by displaced equilibrium reaction against right
according to:
Na2CO3 + H2S -4 Na2S + CO2 + H20
The recovery of chemicals after the quench/melt dissolver would be best done
by keeping a
high suitable operation pressure into the entire chemical recovery cycle as
causticizing,
calcination etc. - which is not cleared by figure.
Black liquor 1 I lA/114A is preheated by the condenser 1 12A of the cooling
medium loop 200
and fed into the reducing, pressurized reaction chamber lA together with
preheated, returned
condensate 20A and oxygen 120 followed by quenching/separation/dissolving of
the
solid/melt phase of recovered chemicals 1 AA by a part of condensate 20A or
another water
containing medium. In order to prevent enrichment of non process elements NPE
into the
circulating condensate 20A a small flow 20AA can be separated. Pressurized
fuel gas/mass
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17
flow 24A of high steam partial pressure, almost moisture saturated, leaves the
reaction
chamber iA and connects expander turbine 6A, which discharge 25A connects
device 10A
for separation of condensate 20A from the fuel gas 26A, which connects
expansion turbine
7A, and the discharge 27A connects device 1 iA for the separation of
condensate 19A from
fuel gas 28A, which condensate is fed counter current into the discharge 25A
and
contaminated hot condensate 20A injects the reaction chamber 1 A. It is an
advantage to
connect the non condensable gases (NCG) 114BB into piping 28A.
From the fuel gas 28A is thus possible to obtain a number of chemicals via a
symbolic shown
device 28AA, after which the fuel gas/rest of fuel gas 28A connects the
combustion chamber
1B of the oxidizing process step for a stoichiometric combustion by compressor
3 supplied air
21 and returned preheated condensate 20B, preferably with an additional fuel
111 B/114B
which has been preheated/vaporized by the condenser 112B of the cooling medium
loop 200.
There is a possibility to distribute the condensate fractions between the
reducing and
oxidizing steps by 19A/B and/or when at an excess to be separated as for
example pulp wash
water. Pressurized flue gas 24B at high steam partial pressure leaves the
combustion
chamber 1 B and enters a gas turbine 4B, when the combustion chamber 1 B
represents a part
of the entire gas turbine neither with it's own shaft and power generator in
accordance with
Figure 15, or as shown by figure in conjunction with the expander turbines,
after which the
discharge 25B connects device l OB for separation of condensate 20B from flue
gas 26B,
which enters expander turbine 7B, and the discharge 27B connects device 11 B
for separation
of condensate 19 from flue gas 28B, which enters expander turbine 8B, and
after which the
discharge 29B, preferably during vacuum, connects device 13B for separation of
cold, clean
condensate excess 16 via barometric fall leg 14 with water seal 15 from cold,
treated flue gas
33 by fan 32. The condensate fraction 19B is preheated by heat
exchanger/condenser 112C
and distributed as 19 A/B and/or 19C. The condensate fractions are stepwise
fed counter
current through the heat exchangers/condensers of the cooling medium loop 200
to be injected
into the reactor chamber 1B etc. according to earlier descriptions.
There is thus a possibility to utilize condensate fractions as 19A/B for pulp
washing, if
necessary for the water balance with the supply of a compensation flow of low
temperature
water, waste water, cold water etc.
There is a possibility to complete/exclude the cooling medium loop 200 by the
preheating/vaporization of liquid natural/bio gas as the additional fuel
111B/114B and/or
oxygen 120, which are fed step wise and counter current the heat exchangers
according to
earlier figures.
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Figure 14
The figure describes the pressurized fuel conversion in stages of at least one
fuel 131 for
driving mobile machine/vehicular/means of transport/craft 41 - a vehicular of
hybrid type
driven by a rotation motor of a quit new motor technology during continuous
combustion.
This pressurized/turbo method comprises compressor 3 for the supply of air
34A/34B, and the
number of expander turbines are three when including at least one step of
steam turbine 5
followed by two turbo expanders 6 and 7. The method also describes a
pressurized fuel cell
2B - corresponding to Figure 12 - by dashed lines, whereby is cleared the
figure comprises
three different arrangements: the entire via both at least one
reaction/combustion chamber 2A
and at least one fuel cell 2B and furthermore either via only reaction chamber
2A or via only
the fuel cell 2B - besides the alternative of an electrically driven hybrid
vehicle.
The figure has the same position markings as previous exemplifications, and by
that follows a
shortened description.
Liquid hydrogen 131 at approx. minus 250 C is passing in series and counter
current the heat
exchangers/vaporizers 115, 116 and l 17 and connects reaction/combustion
chamber 2A
and/or fuel ce112B via connections 133A and 133B respectively. Counter currant
fed fractions
of condensate 17, 18 and 19 connects by pipe 20 reaction/combustion chamber 2A
and/or fuel
cell 2B via piping 20A and 20B respectively. The circulating amount of
condensate 20 is
controlled by the discharge amount of fraction 16. When use of non carbon
content fuels.the
only discharge consisting of clean cold condensate excess 16 and if not use of
oxygen 120 the
compressed air 34 content of nitrogen 33. Generator 36, which can be reversed
to a start
motor as an alternative to a separate one, feeding when necessary
accumulator/battery 39 by
power 45, as a complement to power 45 from the fuel cell 2B, and by that a
possibility for an
alternative electrically driven motor 40.
The discharge only consists of water/condensate and when use of compressed air
the nitrogen
content. The acidification by nitrogen oxides and ground near ozone are both
minimized
thanks to the temperature controlled combustion/oxidation.
Liquid/compressed fuels as hydrogen, and or natural gas in the form of LNG
and/or NGH are
extraordinarily advantageous. Liquid hydrogen expands approx. 840 times when
vaporized.
The method is also use full - by small modifications - for a stationary power
plant
corresponding to Figure 10, which is not cleared by figure.
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19
Figure 15
As a conclusion of the present invention an open system is exemplified by an
integration of a
gas turbine arrangement in the energy conversion first (1) stage.
The combustion chamber 1 of the gas turbine is preferably supplied a preheated
/vaporized
fuel 35/35A, via for example heat exchanger/cooler 115, and compressed air 21
via
compressor 3 of the gas turbine and circulated preheated condensate 20, which
condensate is
injected into the fuel and/or in connection to the combustion chamber 1, after
which
moistened flue gas 22 connects gas turbine 4 for the generation of power 45
via generator 36.
The gas turbine hot discharge of flue gas/stea.m 23 connects some kind of at
least one
steam/intermediate turbine step 5, or similar apparatus of corresponding
function of type
rotating machine, with generator 37 for generation of power 45, and/or direct
as a mass flow
into the expander turbines via dashed line 23/24, for generation of power 45
via generator
38A, when thus discharge 24 or 23/24 connects the expander turbine stages 6, 7
and 8 of the
expansion cooling. When risk for enrichment of impurities/heavy metals etc.
into the
circulating condensate 20, a small flow 20AA is separated.
This figure is also applicable by some modifications for driving
vehicular/means of transport
corresponding to Figure 14, which is not cleared by figure.
Earlier shown heat exchangers 116 and 117 into the discharge of expander
turbines or into the
condensate fractions are also applicable within this figure as well as the
cooling medium loop
200 - which alternatives are not cleared by the figure.
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Comments to the figures
The figures of the present invention are describing the characteristics and
great varieties of the
energy conversion in stages from an overall perspective based on a quit new
system thinking
applicable within the entire energy sector. The conversion in stages in the
state of an open
and/or a closed system during counter currant fed condensate/feed water
fractions, including
the return of preheated condensate/feed water, makes possible the ultimate
energy conversion
during an overall optimization with reference to both environment as economy.
The method facilitates carbon dioxide handling, comprising the final deposit
deep into see or
geological formations and furthermore eliminates the unhealthy discharge of
particles/sub-
microns as well as unburned hydrogen carbons etc. as well as water
steam/aerosols with
corresponding reduction in cloud formation. Fuels which only generate
steam/condensate are
most suitable and especially within the huge transport sector by the
continuous combustion
with rotation motor drive of the invention.
In general there are no transport pumps and control systems shown in any of
the subsequent
figures.
Comments to the extent
= It must be understood that during certain circumstances the oxidation
progress occurs
without any real flame.
= It must be understood that combustion/thermal decomposition complains both
partial/under stoichiometric as total/stoichiometric oxidation, which process
steps can
be used in series_
= It must be understood within the open system produced/utilized pressurized
mass flow
can be as well superheated as moisture saturated or almost moistened_
= It has to be understood both the gas and the steam turbine steps can be
installed as
well before as after the expansion cooling expander turbines.
= It has to be understood some arrangement needs additional condenser capacity
by
external cooling medium.
= It has to be understood the invention also includes so called "sulphur free"
cellulose
processes as well as "causticising freelcausticising reduced needs" recovery
processes.
= The present invention is not restricted to the described performances but
can be varied
within exemplified figures and combined within the scope of the following
patent
claims.
